CA2992428A1 - Incremental hydrogen production from an existing steam/natural gas reformer - Google Patents
Incremental hydrogen production from an existing steam/natural gas reformer Download PDFInfo
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- CA2992428A1 CA2992428A1 CA2992428A CA2992428A CA2992428A1 CA 2992428 A1 CA2992428 A1 CA 2992428A1 CA 2992428 A CA2992428 A CA 2992428A CA 2992428 A CA2992428 A CA 2992428A CA 2992428 A1 CA2992428 A1 CA 2992428A1
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/16—Hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/108—Hydrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/41—Further details for adsorption processes and devices using plural beds of the same adsorbent in series
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/042—Purification by adsorption on solids
- C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0465—Composition of the impurity
- C01B2203/0495—Composition of the impurity the impurity being water
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/06—Integration with other chemical processes
- C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/14—Details of the flowsheet
- C01B2203/146—At least two purification steps in series
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/14—Details of the flowsheet
- C01B2203/146—At least two purification steps in series
- C01B2203/147—Three or more purification steps in series
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
In some aspects, a method for incremental hydrogen production includes separating in a first Pressure Swing Absorption (PSA) system an existing reformer synthesis gas product stream into a first hydrogen stream and a first waste stream. The first waste stream is compressed to at least 40 bar to produce a compressed waste stream. Water is removed from the compressed waste stream to produce a dried waste stream. Carbon dioxide is removed from the dried waste stream to produce a remaining waste stream, and the removed carbon dioxide is at least 85% of carbon dioxide in the existing reformer synthesis gas product stream. A second PSA system separates the remaining waste stream into a second hydrogen stream and a second waste stream, and the second hydrogen stream comprises at least 11% of hydrogen from the existing reformer synthesis gas product stream. The second waste stream is passed to a reformer furnace as fuel gas.
Description
INCREMENTAL HYDROGEN PRODUCTION FROM AN
EXISTING STEAM/NATURAL GAS REFORMER
CLAIM OF PRIORITY
This application claims priority to U.S. Provisional Application No.
62/162,229 filed on May 15, 2015, the entire contents of which are hereby incorporated by reference.
TECHNICAL FIELD
This invention relates to gas-to-liquids production, and more particularly to incremental hydrogen production from an existing steam/natural gas reformer.
io BACKGROUND
An integrated plant for the conversion of a hydrocarbon gas such as natural gas to useful hydrocarbon liquid fuels and feed-stocks comprises an H2+CO syn-gas generation system which provides feed gas to a Fischer-Tropsch catalytic hydrocarbon synthesis system with an associated power and heat energy system.
High efficiency, low capital cost, together with a low carbon footprint, are the major objectives of a total facility. US Patents 6534551 and 6669744 describe an integrated synthesis gas generation system comprising a two-stage synthesis gas generation unit integrated with a gas turbine which provides at least part of the energy required to drive an 02 production plant. The 02 plant can be either a cryogenic air separation unit, a high temperature mixed oxide 02 ion transfer membrane reactor integrated with the gas turbine, or other unit. The two stage synthesis gas generator comprises a Partial Oxidation (PDX) or an Auto-thermal Reformer (ATR) coupled in either case in a parallel or series configuration with a gas heated catalytic steam/hydrocarbon reformer (GHR) in which the heating gas is the mixed product from each synthesis gas generation reactor. The hot exhaust gas from the gas turbine provides at least part of the heat used to preheat the feed streams to the synthesis gas generation reactors.
DESCRIPTION OF DRAWINGS
FIG 1 is an example system for incremental hydrogen production.
Like reference symbols in the various drawings indicate like elements.
DETAILED DESCRIPTION
FIGURE 1 illustrates an example system for incremental hydrogen production.
For example, the process for incremental hydrogen production from an existing catalytic steam/natural gas reformer may use a low-temperature CO2 condensation process to separate the CO2 present in the waste gas from an existing reformer pressure swing adsorption (PSA) hydrogen separation unit so that the remaining hydrogen enriched waste gas may then be sent to a second PSA unit where more Hz can be separated. The waste gas stream 16 may initially be compressed from, for example, about 1.2 bar to 40 bar in the compressor 17 and then the compressed waste gas stream 4 is dried in, for example, an adsorbent bed drier 12, which is regenerated by a nitrogen gas stream 5 and 6. As illustrated, the compressed waste gas steam 7 enters the CO2 condensation system 3 where it is cooled to, for example, within 2 C
of its triple point temperature. The liquid CO2 is separated and evaporated to produce refrigeration for the process and the CO2 product leaves as two separate streams 10 and 11 at an average pressure of about 10bar. The remaining compressed waste gas, stream 8, containing about 65% Hz, is separated in the PSA 2 producing a substantially pure H2 stream 9 at 35bar pressure and a waste gas stream 14 which is used as part of the fuel gas in the existing reformer furnace. In some implementations, the system described can produce an incremental 11% more Hz from the existing reformer synthesis gas product stream 1. The incremental Hz production may use additional natural gas to replace the Hz which would have been burned in the reformer furnace.
The fuel consumption for the incremental Hz production is, in some implementations, 280Btu/scf Hz. In these instances, the produced CO2 in streams 10 plus 11 can be about 85% of the CO2 present in the reformer product stream 1.
A number of embodiments of the invention have been described. Nevertheless, it will be understood that various modifications may be made without departing from the spirit and scope of the invention. Accordingly, other embodiments are within the scope of the following claims.
EXISTING STEAM/NATURAL GAS REFORMER
CLAIM OF PRIORITY
This application claims priority to U.S. Provisional Application No.
62/162,229 filed on May 15, 2015, the entire contents of which are hereby incorporated by reference.
TECHNICAL FIELD
This invention relates to gas-to-liquids production, and more particularly to incremental hydrogen production from an existing steam/natural gas reformer.
io BACKGROUND
An integrated plant for the conversion of a hydrocarbon gas such as natural gas to useful hydrocarbon liquid fuels and feed-stocks comprises an H2+CO syn-gas generation system which provides feed gas to a Fischer-Tropsch catalytic hydrocarbon synthesis system with an associated power and heat energy system.
High efficiency, low capital cost, together with a low carbon footprint, are the major objectives of a total facility. US Patents 6534551 and 6669744 describe an integrated synthesis gas generation system comprising a two-stage synthesis gas generation unit integrated with a gas turbine which provides at least part of the energy required to drive an 02 production plant. The 02 plant can be either a cryogenic air separation unit, a high temperature mixed oxide 02 ion transfer membrane reactor integrated with the gas turbine, or other unit. The two stage synthesis gas generator comprises a Partial Oxidation (PDX) or an Auto-thermal Reformer (ATR) coupled in either case in a parallel or series configuration with a gas heated catalytic steam/hydrocarbon reformer (GHR) in which the heating gas is the mixed product from each synthesis gas generation reactor. The hot exhaust gas from the gas turbine provides at least part of the heat used to preheat the feed streams to the synthesis gas generation reactors.
DESCRIPTION OF DRAWINGS
FIG 1 is an example system for incremental hydrogen production.
Like reference symbols in the various drawings indicate like elements.
DETAILED DESCRIPTION
FIGURE 1 illustrates an example system for incremental hydrogen production.
For example, the process for incremental hydrogen production from an existing catalytic steam/natural gas reformer may use a low-temperature CO2 condensation process to separate the CO2 present in the waste gas from an existing reformer pressure swing adsorption (PSA) hydrogen separation unit so that the remaining hydrogen enriched waste gas may then be sent to a second PSA unit where more Hz can be separated. The waste gas stream 16 may initially be compressed from, for example, about 1.2 bar to 40 bar in the compressor 17 and then the compressed waste gas stream 4 is dried in, for example, an adsorbent bed drier 12, which is regenerated by a nitrogen gas stream 5 and 6. As illustrated, the compressed waste gas steam 7 enters the CO2 condensation system 3 where it is cooled to, for example, within 2 C
of its triple point temperature. The liquid CO2 is separated and evaporated to produce refrigeration for the process and the CO2 product leaves as two separate streams 10 and 11 at an average pressure of about 10bar. The remaining compressed waste gas, stream 8, containing about 65% Hz, is separated in the PSA 2 producing a substantially pure H2 stream 9 at 35bar pressure and a waste gas stream 14 which is used as part of the fuel gas in the existing reformer furnace. In some implementations, the system described can produce an incremental 11% more Hz from the existing reformer synthesis gas product stream 1. The incremental Hz production may use additional natural gas to replace the Hz which would have been burned in the reformer furnace.
The fuel consumption for the incremental Hz production is, in some implementations, 280Btu/scf Hz. In these instances, the produced CO2 in streams 10 plus 11 can be about 85% of the CO2 present in the reformer product stream 1.
A number of embodiments of the invention have been described. Nevertheless, it will be understood that various modifications may be made without departing from the spirit and scope of the invention. Accordingly, other embodiments are within the scope of the following claims.
2
Claims (2)
1. A method for incremental hydrogen production, comprising:
separating in a first Pressure Swing Absorption (PSA) system an existing reformer synthesis gas product stream into a first hydrogen stream and a first waste stream;
compressing the first waste stream to at least 40 bar to produce a compressed waste stream;
removing water from the compressed waste stream to produce a dried waste stream;
removing carbon dioxide from the dried waste stream to produce a remaining waste stream, wherein the removed carbon dioxide is at least 85% of carbon dioxide in the existing reformer synthesis gas product stream;
separating in a second PSA system the remaining waste stream into a second hydrogen stream and a second waste stream, wherein the second hydrogen stream comprises at least 11% of hydrogen from the existing reformer synthesis gas product stream; and passing the second waste stream to a reformer furnace as fuel gas.
separating in a first Pressure Swing Absorption (PSA) system an existing reformer synthesis gas product stream into a first hydrogen stream and a first waste stream;
compressing the first waste stream to at least 40 bar to produce a compressed waste stream;
removing water from the compressed waste stream to produce a dried waste stream;
removing carbon dioxide from the dried waste stream to produce a remaining waste stream, wherein the removed carbon dioxide is at least 85% of carbon dioxide in the existing reformer synthesis gas product stream;
separating in a second PSA system the remaining waste stream into a second hydrogen stream and a second waste stream, wherein the second hydrogen stream comprises at least 11% of hydrogen from the existing reformer synthesis gas product stream; and passing the second waste stream to a reformer furnace as fuel gas.
2. A system for incremental hydrogen production, comprising:
a first Pressure Swing Absorption (PSA) system configured to separate an existing reformer synthesis gas product stream into a first hydrogen stream and a first waste stream;
a compressor configured to compress the first waste stream to at least 40 bar to produce a compressed waste stream;
a drier configured to remove water from the compressed waste stream to produce a dried waste stream;
a low-temperature separator configured to remove carbon dioxide from the dried waste stream to produce a remaining waste stream, wherein the removed carbon dioxide is at least 85% of carbon dioxide in the existing reformer synthesis gas product stream;
a second PSA system configured to separate the remaining waste stream into a second hydrogen stream and a second waste stream, wherein the second hydrogen stream comprises at least 11% of hydrogen from the existing reformer synthesis gas product stream; and a conduit configured to pass the second waste stream to a reformer furnace as fuel gas.
a first Pressure Swing Absorption (PSA) system configured to separate an existing reformer synthesis gas product stream into a first hydrogen stream and a first waste stream;
a compressor configured to compress the first waste stream to at least 40 bar to produce a compressed waste stream;
a drier configured to remove water from the compressed waste stream to produce a dried waste stream;
a low-temperature separator configured to remove carbon dioxide from the dried waste stream to produce a remaining waste stream, wherein the removed carbon dioxide is at least 85% of carbon dioxide in the existing reformer synthesis gas product stream;
a second PSA system configured to separate the remaining waste stream into a second hydrogen stream and a second waste stream, wherein the second hydrogen stream comprises at least 11% of hydrogen from the existing reformer synthesis gas product stream; and a conduit configured to pass the second waste stream to a reformer furnace as fuel gas.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US201562162229P | 2015-05-15 | 2015-05-15 | |
| US62/162,229 | 2015-05-15 | ||
| PCT/US2016/032716 WO2016187125A1 (en) | 2015-05-15 | 2016-05-16 | Incremental hydrogen production from an existing steam/natural gas reformer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2992428A1 true CA2992428A1 (en) | 2016-11-24 |
Family
ID=56133029
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA2992428A Abandoned CA2992428A1 (en) | 2015-05-15 | 2016-05-16 | Incremental hydrogen production from an existing steam/natural gas reformer |
Country Status (7)
| Country | Link |
|---|---|
| US (1) | US9914643B2 (en) |
| EP (1) | EP3294670B1 (en) |
| CN (1) | CN107848795B (en) |
| AU (1) | AU2016265832A1 (en) |
| CA (1) | CA2992428A1 (en) |
| ES (1) | ES2769724T3 (en) |
| WO (1) | WO2016187125A1 (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9914643B2 (en) | 2015-05-15 | 2018-03-13 | Gtlpetrol Holding Co. Llc | Incremental hydrogen production from an existing steam/natural gas reformer |
| EA039539B1 (en) | 2016-11-09 | 2022-02-08 | 8 Риверз Кэпитл, Ллк | Method for power production with integrated production of hydrogen |
| AU2020292848A1 (en) | 2019-06-13 | 2022-02-03 | 8 Rivers Capital, Llc | Power production with cogeneration of further products |
| CN110817794B (en) * | 2019-10-28 | 2023-08-01 | 中科液态阳光(苏州)氢能科技发展有限公司 | Hydrogen separation and water gas reforming integrated ultrahigh pressure hydrogen production system and method thereof |
| CN110790229B (en) * | 2019-10-28 | 2023-08-01 | 中科液态阳光(苏州)氢能科技发展有限公司 | Methanol water ultrahigh pressure hydrogen production system and hydrogen production method thereof |
| AU2022386713A1 (en) | 2021-11-15 | 2024-05-02 | Topsoe A/S | Blue hydrogen process and plant |
| WO2023089571A1 (en) | 2021-11-18 | 2023-05-25 | 8 Rivers Capital, Llc | Method for hydrogen production |
| WO2024104905A1 (en) | 2022-11-16 | 2024-05-23 | Topsoe A/S | Plant and process for producing hydrogen with improved operation of a low temperature co2 removal unit |
Family Cites Families (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6669744B2 (en) | 1998-04-14 | 2003-12-30 | Air Products And Chemicals, Inc. | Process and apparatus for the production of synthesis gas |
| GB0025150D0 (en) | 2000-10-13 | 2000-11-29 | Air Prod & Chem | A process and apparatus for the production of synthesis gas |
| AU748793B2 (en) | 1998-11-10 | 2002-06-13 | Fluor Technologies Corporation | Recovery of CO2 and H2 from PSA offgas in an H2 plant |
| US7449167B2 (en) * | 2004-07-08 | 2008-11-11 | Air Products And Chemicals, Inc. | Catalyst and process for improving the adiabatic steam-reforming of natural gas |
| FR2877939B1 (en) | 2004-11-16 | 2007-02-02 | Air Liquide | PROCESS AND PLANT FOR THE COMBINED PRODUCTION OF HYDROGEN AND CARBON DIOXIDE |
| AU2009215419B2 (en) * | 2008-02-20 | 2014-01-09 | Gtlpetrol Llc | Systems and processes for processing hydrogen and carbon monoxide |
| US20100037521A1 (en) * | 2008-08-13 | 2010-02-18 | L'Air Liquide Societe Anonyme Pour L'Etude et l'Exploitatation Des Procedes Georges Claude | Novel Steam Reformer Based Hydrogen Plant Scheme for Enhanced Carbon Dioxide Recovery |
| AU2009283902B2 (en) * | 2008-08-21 | 2015-07-09 | NiQuan Energy LLC | Systems and processes for producing ultrapure, high pressure hydrogen |
| US8394174B2 (en) * | 2009-05-18 | 2013-03-12 | American Air Liquide, Inc. | Processes for the recovery of high purity hydrogen and high purity carbon dioxide |
| FR2953505B1 (en) * | 2009-12-03 | 2012-02-10 | Air Liquide | PROCESS FOR THE PRODUCTION OF HYDROGEN COMBINED WITH CARBON DIOXIDE CAPTURE |
| FR2961802A1 (en) | 2010-06-29 | 2011-12-30 | Air Liquide | Combined production of hydrogen and carbon dioxide from hydrocarbon mixture comprises e.g. reforming hydrocarbon mixture to give synthesis gas, cooling the gas, oxidation reaction, cooling and drying the gas and separating the gas |
| US9914643B2 (en) | 2015-05-15 | 2018-03-13 | Gtlpetrol Holding Co. Llc | Incremental hydrogen production from an existing steam/natural gas reformer |
-
2016
- 2016-05-16 US US15/155,715 patent/US9914643B2/en active Active
- 2016-05-16 CN CN201680041627.9A patent/CN107848795B/en active Active
- 2016-05-16 ES ES16729660T patent/ES2769724T3/en active Active
- 2016-05-16 CA CA2992428A patent/CA2992428A1/en not_active Abandoned
- 2016-05-16 AU AU2016265832A patent/AU2016265832A1/en not_active Abandoned
- 2016-05-16 EP EP16729660.7A patent/EP3294670B1/en active Active
- 2016-05-16 WO PCT/US2016/032716 patent/WO2016187125A1/en active Application Filing
Also Published As
| Publication number | Publication date |
|---|---|
| EP3294670A1 (en) | 2018-03-21 |
| CN107848795B (en) | 2021-03-26 |
| AU2016265832A1 (en) | 2018-02-01 |
| ES2769724T3 (en) | 2020-06-29 |
| US9914643B2 (en) | 2018-03-13 |
| US20170101313A1 (en) | 2017-04-13 |
| WO2016187125A1 (en) | 2016-11-24 |
| CN107848795A (en) | 2018-03-27 |
| EP3294670B1 (en) | 2019-10-23 |
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